Method and system for efficiently disposing of dead animal parts and for converting animal parts and biomass to fuels

ABSTRACT

A method and system utilizes animal parts as a feedstock to produce one or more combustible fuels or chemicals. The animal parts are mixed with a chemical waste to form an animal-chemical waste product. This animal-chemical waste product is transferred to a reactor and heated under pressure to form a gaseous composition. The gaseous composition is distilled to form one or more combustible fuels.

FIELD OF THE INVENTION

The present invention relates to forming combustible fuels from biomass,and more particularly to a system for eliminating waste animal parts byutilizing the animal parts as a feedstock for producing combustiblefuels through a distillation process.

BACKGROUND OF THE INVENTION

The management and disposal of animal parts is a huge problem throughoutthe world. It is a particular problem for chicken and turkey processorsas well as swine and cattle slaughterhouses. In the process ofslaughtering animals and preparing them for market, there is a greatdeal of waste parts such as blood, bones, organs, and skin that must bedisposed. Efficiently dealing with the sheer magnitude of animal partsis problematic, but doing so in compliance with local, state and federalregulations is even more challenging.

In recent years, considerable attention has been given to the conversionof corn and other plant material to liquid fuels. The use of plantmaterial and other biomass offers the potential to replace or supplementdwindling reserves of non-renewable fossil fuels with fuels derived frombiomass types of material which contains carbon and are renewable. If,in the case of dead animal parts, it is possible to convert them tofuels and at the same time provide an efficient and effective means ofdisposal, then the utility and advantages of such are clear.

SUMMARY OF THE INVENTION

The present invention entails an efficient method of managing anddisposing dead animal parts. The method entails transferring parts ofone or more dead animals into a reactor and pressurizing the reactorwith an inert gas such as argon, nitrogen or helium. The reactor isheated for a selected period of time and this transforms at least aportion of the dead animal parts into a gaseous composition.

The present invention also entails a method of forming a fuel orchemical from animal parts. The animal parts are transferred into areactor and heated. In the process, a portion of the dead animal partsare transformed into a gaseous composition. Once the gaseous compositionis formed it is distilled and in the distillation process one or morecombustible fuels is formed.

In one particular embodiment of the present invention, the dead animalparts are mixed with a chemical reactant or a chemical waste. Thechemical reactant or chemical waste is mixed with the dead animal partsto form an animal-chemical waste product. This product is transferred toa reactor that is pressurized with an inert gas such as argon, nitrogenor helium. The reactor is heated and at least a portion of the deadanimal parts is transformed to a gaseous composition that is directed toa distillation process. During the course of the distillation process,the gaseous composition formed from the dead animal parts is cooled andcondensed to form a fuel or chemical.

Other objects and advantages of the present invention will becomeapparent and obvious from a study of the following description and theaccompanying drawings which are merely illustrative of such invention.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic illustration of the distillation system of thepresent invention that can be used to convert animal parts to fuels.

FIG. 2 is a flow chart that illustrates basic steps in converting animalparts to a combustible fuel.

DESCRIPTION OF THE INVENTION

With further reference to the drawing, a distillation system is showntherein and indicated generally by the numeral 10. As will beappreciated from subsequent portions of this disclosure, distillationsystem 10 can be utilized to convert animal parts and biomass in generalto various types of combustible fuels and other chemicals of economicinterest. Before discussing the method or process of converting animalparts and biomass to fuels and other combustible chemicals, thedistillation system 10 will be described.

Forming a part of the distillation system 10 is a feedstock storage tank12 and a chemical reactant storage tank 14. Feedstock storage tank 12serves to receive and hold animal parts or other biomass. Storage tank12 receives and holds various types and forms of organic chemicals orchemical waste that, as will be appreciated from subsequent portions ofthe disclosure, is mixed with the animal parts and/or biomass to form ananimal-chemical waste product.

Both feedstock tank 12 and the chemical waste storage tank 14 arecommunicatively connected to a holding tank or chamber 16. Also,communicatively connected with the holding chamber 16 is a base storagetank 18. A conduit is connected between the base storage tank 18 and theholding tank 16. A control valve 20 is connected between the basestorage tank 18 and the holding tank 16 for metering base into theholding tank.

A reactor 22 also forms a part of the distillation system 10. A conduit17 extends between the holding tank 16 and the reactor 22. A pump 19 iscommunicatively connected to the conduit 17 for pumping theanimal-chemical waste product or mixture from the holding tank 16 to thereactor 22. In addition, conduit 17 is provided with a shut-off valve 21for controlling the flow of the animal-chemical waste product from theholding tank 16 to the reactor 22.

Reactor 22 is designed to be pressurized and to heat the contentsthereof. Two types of heating provisions are provided in associationwith the reactor 22. First, reactor 22 is provided with an externalheating capability. That is, reactor 22 is provided with externalheating elements that are disposed within or adjacent an outer jacket24. In addition, there is provided one or more internal heating elements26 that project into the reactor 22. As will be appreciated fromsubsequent portions of the disclosure, the external heating device andthe internal heating elements 26 can be controlled during the course ofthe distillation process to cause the animal-chemical waste product tovaporize and to produce a vapor. Furthermore, reactor 22 is providedwith a temperature gauge 30 and a pressure gauge 32. The temperaturegauge can measure the temperature of the animal-chemical waste containedwithin the reactor 22, or alternatively, the temperature gauge canreflect the temperature of the inner wall of the reactor 22.

Distillation system 10 is provided with an inert gas storage tank 34.Gas storage tank 34 is communicatively connected to the reactor 22. Aconduit extends from the gas storage tank 34 to the reactor 22. Disposedwithin the conduit is a control valve 36 for metering gas from the gasstorage tank 34 to the reactor 22. Further, reactor 22 includes anoutlet 38 formed in the bottom or in the bottom portion thereof. Duringthe course of the distillation process fuel product will accumulate inthe bottom of the reactor 22 and from time to time this fuel product canbe discharged via the outlet 28 and captured. As will be appreciatedfrom subsequent portions of the disclosure, the fuel product andchemical components discharged through outlet 28 will differ from fueland chemical products discharged downstream or subsequently in thedistillation process.

Distillation system 10 also includes a series of distillation tanksand/or evaporation tanks or towers. In the case of the distillationsystem disclosed in FIG. 1, there is provided a first distillation tank40. Extending between the first distillation tank 40 and the reactor 22is a conduit 38. A valve 39 is provided between the distillation tank 40and the reactor 22 for controlling the passage of vapor or superheatedliquid from the reactor 22 to the first distillation tank 40.Distillation tank 40 includes an outlet 42. A second fuel product, andcomponent chemicals of economic interest, can be discharged via outlet42. Additionally the first distillation tank 40 includes a pressuregauge 44 for indicating the pressure within distillation tank 40.

A second distillation tank 50 is provided downstream of the firstdistillation tank 40. A transfer conduit 46 extends between thedistillation tanks 40 and 50. A control valve 48 controls the transferof vapor or other material from the first distillation tank 40 to thesecond distillation tank 50. Second distillation tank 50 includes aproduct outlet 52. A pressure gauge 54 indicates the pressure withindistillation tank 50. Distillation tank 50 can, and usually does,produce a fuel product, and component chemicals of economic interest,that are different from the fuel products that are discharged viaoutlets 28 and 42. This will be further explained subsequently herein.

Extending from distillation tank 50 is a conduit 60. Disposed within theconduit 60 is a control valve 62 for controlling the flow of vapor orsuperheated liquid from the distillation tank 50 into and through theconduit 60. Conduit 60 leads to a cooling tower or evaporation tank,indicated generally by the numeral 70. As will be appreciated fromsubsequent portions of this disclosure, the evaporation tank 70 includesa series of outlets numbered 72, 74, 76, 78, 80, 82, 84 and 86 that arevertically spaced along a sidewall of the evaporation tank 70. Vaporproduced in the reactor 22 and ultimately introduced into the lowerportion of the evaporation tank, will move upwardly in a conventionalfashion. In the process condensation occurs and various types of fuelsand chemicals will be captured in the evaporation tank and dischargedout through the various outlets 72-86 provided therein.

Turning to the process of the present invention, a biomass feedstock isutilized. In a preferred process the feedstock comprises animal partsfrom chickens, turkeys, pigs, cows, dogs, horses and other animals. Itis contemplated that one source for the feedstock would be animalslaughterhouses which typically produce large amounts of waste bodyparts, waste sludge, and washed down wastewater that results fromslaughterhouse cleaning. These animal waste parts and related animalwaste compositions are usually subjected to a grinding, chopping, orcutting operation. That is, the animal parts are ground or cut intosmaller parts by a meat grinder, hammermill, or other apparatus.

The animal feedstock can be augmented with plant organic matter, soybeanoils, corn, corn oils, rapeseed oils, palm fruit, and other plant orvegetable stock. In any event, the feedstock is held within thefeedstock tank 12. Preferably the feedstock tank 12 is sealed so as tocontrol odor and bacteria. A blanket of nitrogen can be confined in theheadspace at a pressure of approximately one atmosphere. While the sizeof the feedstock tank 12 can vary, it should be sized to containsufficient feedstock to support the process for one day.

An organic chemical reactant, such as a chemical waste, is mixed withthe animal feedstock to form an animal-chemical waste product. A rangeof organic chemicals or chemical waste products can be utilized.Typically they would include industrial organic waste that is producedin commercial and industrial facilities. For example, a suitablechemical waste product would comprise polymer waste that typicallycontains components such as propanoic acid and its esters, hexanal, etc.In addition, other chemical waste suitable for mixing with the animalfeedstock includes chemicals such as methacrylates, hexanes, methylpentanes, ethanol, hexahydrogenzene, etc. Other chemical waste productscan be used and various types of chemical waste can be blended. As willbe discussed subsequently herein, the composition of the chemicalreactant or waste utilized will affect the nature and quality of thefuel or chemical produced. It is hypothesized that the more effectivechemical reactant or waste products would be characterized in that theywill have a relatively high pH and a sufficient carbon content to drivechemical reactions throughout the process to be described subsequentlyherein. Organic acids, methyl esters, and most non-hazardous chemicaland polymer wastes are desirable. Even waste petroleum products such aspaint thinners, gasoline, diesel fuel, kerosene, jet fuel, and aviationgasoline that is recovered from contaminated sites can be used as awaste chemical or blended with other waste chemicals for use in thisprocess.

In two tests conducted, two batches of chemical waste products wereused. In one test, a mixture of propenoic acid and guaiccol were used.The proportions of the components of the waste are not deemed criticalto the basic process. It is acknowledged that the resulting fuels andchemicals can be varied based on the selection and amounts of theparticular waste components utilized. In another test a mixture ofacetic acid, butyl ester, hexahydrobenzene, cyclopentane,methyl-formamide, N, N-dimethyl and oxolane was used as a chemical wasteproduct.

The chemical reactant or waste products are conveyed into a receivingtank 14. From time to time, the animal feedstock in tank 12 and thechemical waste product held in tank 14 are conveyed into the holdingtank 16. The holding tank may include an agitator or mixer that mixesthe animal feedstock with the chemical waste to form the animal-chemicalwaste product. To facilitate reactions in the distillation system 10 itis believed that the pH of the animal-chemical waste mixture should becontrolled to a pH of approximately 8 to 12. To control the pH to adesired level, a base contained within the base storage tank isselectively metered into the holding tank 16 and mixed with theanimal-chemical waste mixture. Suitable bases for mixing with theanimal-chemical waste mixture are sodium hydroxide, potassium hydroxide,etc. Any strong base will work with this system.

After transferring the animal-chemical waste to the reactor 22, thereactor is cleaned by a gas purging procedure. By opening valve 36, aninert gas from tank 34 is directed into the reactor 22. Various gasessuch as nitrogen, helium and argon can be used. Argon maybe preferred.During a portion of the purging operation, the reactor 22 is vented.During this purging operation it is contemplated that reactor 22 wouldbe slightly pressurized with the argon gas with the pressure being inthe range of 5-6 psi. The purging gas can also be directed through thereactor 22 and through tanks 40 and 50 as well as through theevaporation tank 70. This will effectively clean the reactor and tanksand will contribute to efficient and effective chemical reactions duringthe entire process. After purging, the reactor 22 is closed andpressurized to a level of approximately 40-80 psi with argon gas.Thereafter the animal-chemical waste mixture is pumped by pump 19 fromthe holding tank 16 through line 17 and valve 21 into the reactor 22.Because the animal parts have been chopped, cut or ground, theanimal-chemical waste mixture typically assumes a slurry consistency.

Thus, the animal-chemical waste mixture in the reactor 22 will be heldin a pressurized argon or inert gas environment. In the case of argon,it is believed that the argon functions as a medium for variousreactants to mix, and provides consistency and predictability in thevarious chemical reactions that will take place in the reactor 22. Inaddition, the argon will increase the boiling point of theanimal-chemical waste mixture.

Once the animal-chemical waste mixture has been directed into thereactor 22, and the reactor is pressurized with an inert gas, thereactor is heated. Reactor 22, as discussed above, has two sources ofheat. First, the reactor is provided with an external heating system ordevice that is incorporated into the jacket 24 of the heater. Theanimal-chemical waste mixture is first heated by the external heatingsystem or device. The external heating system will be utilized to raisethe temperature of the reactor to a temperature of 200° C. to 290° C. Asthe temperature of the reactor 22 is increased, so will the pressure inthe reactor. It is contemplated that with a temperature increase in therange of 200° C. to 290° C. that the pressure within the reactor 22 willincrease to approximately 90-350 psi. Upon reaching 350 psi, orthereabouts, it is contemplated that the reactor would be vented so asto reduce the pressure within the reactor to a pressure of 350 psi orbelow.

During the course of heating the reactor 22 by the external heat source,as noted above, the internal pressure within the reactor 22 willincrease. Once the internal pressure begins to increase within the rangeof 90-350 psi, then the internal heating element or elements 26 can beactuated. Internal heating element or elements 26 are preferablyintermittently utilized to heat the animal-chemical waste mixture. Asshown in FIG. 1 the internal heating element or elements 26 project intothe mixture. In one typical operation, the internal heating element orelements 26 would be switched on and off with the ON time constitutingapproximately 30% of the time and the OFF time constitutingapproximately 70% of the time.

Once the reactor 22 reaches a temperature of 200° C. to 290° C. then amultitude of reactions will begin taking place. As the animal-chemicalwaste mixture is heated in the presence of argon and under the pressureof 90-350 psi, a series of reactions will take place and these reactionswill produce a gaseous composition or vapor along with a super hotliquid. It is contemplated that the residency time of theanimal-chemical waste product within the reactor at a temperature of200° C. to 290° C. and at a pressure of 90-350 psi will be in the rangeof 1 to 5 hours.

After a selected residency time, the valve 39 disposed between thereactor 22 and the first distillation tank 40 is open. The gaseouscomposition produced in the reactor 22 is permitted to flow from thereactor 22 through the conduit 38 into the distillation tank 40. Detailsof the distillation tanks are not shown herein in detail because such isnot per se material to the present invention, and further, suchdistillation tanks are well known and widely used for condensing gaseouscompositions. In any event, as the gaseous composition from the reactor22 moves vertically and upward through the distillation tank 40,portions of the gaseous composition will condense and the condensedportion will be directed to outlet 42. While the precise chemicalcomposition of the distillate will vary depending upon the feedstock,the chemical waste, the inert or noble gas used, and certain otheroperating parameters of the reactor, the distillate will comprise acombustible fuel and other chemicals.

In a typical distillation process of the type described in FIG. 1, allof the gaseous composition passing through distillation tank 40 may notbe condensed. Thus, some of the gaseous composition passing throughdistillation tank 40 can be directed through conduit 46 and valve 48into the second distillation tank 50. Here, as the gaseous compositionmoves vertically and upwardly through the distillation tank 50, portionsof the gaseous composition will condense to form a distillate, which isdischarged from outlet 52. Again, while the precise composition of thedistillate discharged from outlet 52 will vary based on the factorsdiscussed above, the distillate produced will again be a combustiblefuel and other chemicals of economic value.

In some cases there may remain an uncondensed gaseous composition in thesecond distillation tank 50. In that case the remaining gaseouscomposition is directed through conduit 60, control valve 62 to theevaporation tank or tower 70. Again, details of the evaporation tank 70are not dealt with herein because such is not per se material to thepresent invention, and further, such structures are commonly used andwell understood by those skilled in the art. In any event, the gaseouscomposition entering the evaporation tank 70 will be directed into thebottom thereof. Upon entry to the evaporation tank 70, the gaseouscomposition will spiral upwardly through the evaporation tank. Atcertain points along the way portions of the vapor or gaseouscomposition will condense. The evaporation tank, at various heightintervals, is provided with plates to catch the various distillates. Asillustrated in FIG. 1, at various height intervals along the evaporationtank 70, there is provided a series of discharge outlets 74-86. As thevapor or gaseous composition moves upwardly through the evaporation tank70, at certain points along the way certain distillates will be producedand discharged from the respective outlets 74-86.

In the example discussed above and shown in FIG. 1, the quality of thedistillates produced by this distillation process will vary dependingupon the location where the distillate is discharged from the system.For example, the product discharged from the outlet 28 associated withthe reactor will differ substantially in quality from the distillateproduced at the outlet 86 of the evaporation tank 70. Generally, themore refined and lighter fuel oils and chemical compositions will beformed later on in the distillation process.

The range of combustible fuels or chemicals produced by the distillationprocess discussed above, include crude oil, biogel, biodiesel and otherbio fuels, and common industrially used chemicals. As used herein, theterm “fuel” means a conventional fuel or a flammable chemical. A seriesof tests were conducted utilizing ground chicken parts and two generaltypes of chemical waste. In one test the chemical waste includedpropenoic acid and guaiccol. In another test the chemical waste includeda mixture of acetic acid, butyl ester, hexahydrobenzene, cyclopentane,methyl-formamide, N, N-dimethyl oxolane. Listed below is a partial listof the fuel and chemical products collected at various collection sitesin the system.

Partial List of Products Collected at tank “40”

-   -   1-Propanol, 2-methyl-    -   2- Propanol    -   Camphene    -   Decane, 5- methyl    -   Hexane    -   Pentane,2,3,3-trimethyl    -   Avantin

Partial List of Products Collected at tank “39”

-   -   Benzene, 1,2,4- trimethyl    -   O-xylol    -   Benzene,ethyl- Phenylethane    -   Cyclohexanol    -   Dodecanoic acid methyl ester    -   Hexanal    -   Pentane, 3-ethyl-    -   Methacide

Partial List of Products Collected at tank “70”

-   -   Benzene, ethyl-    -   Decane    -   Dodecane    -   Heptane, 4-methyl-    -   Octanoic acid, methyl ester    -   Ethanol, 2-propoxy    -   Phenol    -   Ethanol    -   Ethyl Cyclobutane    -   Cyclohexane    -   2- Propenoic acid, 2- methyl, methyl ester    -   2,3,3 Trimethyl pentane    -   2- methyl nonane    -   Undecane    -   Dodecane    -   Butane    -   Camphene    -   Decane    -   2- Propanol    -   2,6- Dimethyl octane    -   2,5 Dimethyl Octane    -   Butane    -   Ethanol    -   Cyclohexane    -   Trimethylpentane    -   Trimethylhexane    -   Pinene    -   Decane    -   Limonene

Partial List of Products Collected at tank “26”

-   -   1- Heptene    -   Acintene A    -   Naxol

1. A method of forming fuel from animal parts, comprising: a. utilizinganimal parts as a feedstock; b. mixing a chemical reactant with theanimal parts to form an animal-chemical waste product; c. transferringthe animal-chemical waste product to a reactor; d. heating theanimal-chemical waste product in the reactor under pressure to form agaseous composition; and e. distilling the gaseous composition to formcombustible fuel.
 2. The method of claim 1 wherein the feedstockcomprises fowl.
 3. The method of claim 1 wherein the feedstock furtherincludes plant parts.
 4. The method of claim 3 wherein the animal partsand plant parts that comprise the feedstock are taken from the groupconsisting of fowl, pigs, cows, horses, dogs, coconut shells, husks,palm fruit, rapeseed oil, sunflower seed oil, corn oil and soybean oilextracts.
 5. The method of claim 1 including controlling the pH of theanimal-chemical waste product.
 6. The method of claim 5 whereincontrolling the pH includes varying the amount of chemical reactantadded to the feedstock.
 7. The method of claim 5 including controllingthe pH to about 8-12.
 8. The method of claim 5 wherein controlling thepH of the animal-chemical waste product includes adding a base to theanimal-chemical waste product.
 9. The method of claim 1 includingpressurizing the reactor with a noble or inert gas.
 10. The method ofclaim 9 wherein the inert gas is taken from the group consisting ofargon, nitrogen, and helium.
 11. The method of claim 1 includingpressurizing the reactor to about 40 to 80 psi with a noble or inert gastaken from the group consisting of argon, nitrogen and helium.
 12. Themethod of claim 11 including pressurizing the reactor with argon. 13.The method of claim 12 including heating the animal-chemical wasteproduct after the reactor has been pressurized.
 14. The method of claim13 including heating the animal-chemical waste product in the reactor toa temperature of approximately 200 to 290° C.
 15. The method of claim 1including heating the animal-chemical waste product to a temperature ofapproximately 200 to 290° C.
 16. The method of claim 1 including amultistage distilling process where the gaseous composition passes intoor through a series of distilling or condensing devices.
 17. The methodof claim 16 including at least three condensing devices arranged inseries.
 18. The method of claim 1 including grinding or cutting theanimal parts to form a ground mixture of animal parts and combining theground mixture of animal parts with the chemical reactant.
 19. Themethod of claim 1 including purging the reactor by directing a gasselected from the group consisting of argon, nitrogen and helium throughthe reactor.
 20. The method of claim 1 wherein the chemical reactantincludes a chemical waste.
 21. The method of claim 20 wherein thechemical waste is taken from the group consisting of propenoic acid,guaiccol, acetic acid, butyl ester, hexahydrobenzene, cyclopentane,methyl-formamide, N, N-dimethyl oxioane.
 22. The method of claim 1including grinding the animal parts to where the animal parts become afluid slurry.
 23. A method of forming fuel from animal parts comprising:a. utilizing animal parts as a feedstock; b. transferring the animalparts to a reactor; c. transferring a gas selected from the groupconsisting of argon, nitrogen and helium into the reactor; d. heatingthe animal parts in the reactor under pressure to form a gaseouscomposition; and e. distilling the gaseous composition produced by theanimal parts to form combustible fuel.
 24. The method of claim 23wherein the gas transferred into the reactor is argon.
 25. The method ofclaim 23 including pressurizing the gas within the reactor.
 26. Themethod of claim 25 wherein the gas in the reactor is pressurized toabout 40 to 80 psi.
 27. The method of claim 23 wherein the animal partsare taken from the group consisting of chicken parts, pig parts, and cowparts.
 28. The method of claim 23 further including mixing a chemicalwaste or reactant with the animal parts to form an animal-chemical wasteproduct; and wherein the animal-chemical waste product is transferredinto the reactor and after heating produces the gaseous composition thatis distilled.
 29. The method of claim 28 wherein the chemical waste orreactant is taken from the group consisting of propenoic acid, guaiccol,acetic acid, butyl ester, hexahydrobenzene, cyclopentane,methyl-formamide, N, N-dimethyl oxloane.
 30. The method of claim 23including heating the reactor to a temperature of approximately 200 to290° C.
 31. The method of claim 30 including heating the animal parts inthe reactor for a time period of 1 to 5 hours.
 32. The method of claim23 including producing a combustible fuel within the reactor, and aftera selected period of heating the animal parts in the reactor, removingthe combustible fuel from the reactor.
 33. The method of claim 23wherein the method of forming the fuels from animal parts is carried outin a distilling system including a series of condensing units, andwherein the gaseous composition is directed from the reactor to andthrough one or more of the condensing units where portions of thegaseous composition condense and form one or more combustible fuels. 34.The method of claim 23 including heating the contents of the reactorwith one or more internal heating devices and one or more externalheating devices.
 35. The method of claim 34 including intermittentlyactuating the one or more internal heating elements.
 36. A method offorming fuel from animal or plant parts comprising: a. utilizing abiofeed stock that is formed from animal or plant parts; b. transferringthe biofeed stock to a reactor; c. pressurizing the reactor with argon;d. heating the biofeed stock in the reactor to produce a gaseouscomposition; and e. distilling the gaseous composition to form fuelcompositions and chemicals.
 37. The method of claim 36 includingpressurizing the reactor with argon to a pressure of approximately 40-80psi.
 38. The method of claim 37 including purging and cleaning thereactor by directing argon into or through the reactor and thereafterpressurizing the reactor with argon to a pressure of approximately 40-80psi.
 39. The method of claim 36 wherein the method is carried out in adistilling system having a series of condensing units communicativelyconnected, directly or indirectly, with the reactor.
 40. The method ofclaim 39 including purging the reactor and at least one of thecondensing units with a noble or inert gas selected from the groupconsisting of argon, nitrogen and helium.
 41. The method of claim 40wherein the purging gas is argon.
 42. The method of claim 36 includingheating the biofeedstock in the reactor to a temperature ofapproximately 200 to 290° C.
 43. The method of claim 36 including mixinga chemical waste or reactant with the biofeedstock to form abiofeed-chemical waste product that is transferred to the reactor.
 44. Amethod of disposing of parts of dead animals comprising: transferringthe parts of the dead animal into a reactor; pressurizing the reactorwith an inert gas; and heating the parts of the dead animals andtransforming at least a portion of the parts of the dead animals into agaseous composition.
 45. The method of claim 44 including pressurizingthe reactor with argon.
 46. The method of claim 44 wherein the inert gasis taken from the group consisting of argon, nitrogen, and helium. 47.The method of claim 44 including pressurizing the reactor to about 40 to80 psi with the inert gas and wherein the inert gas is taken from thegroup consisting of argon, nitrogen and helium.
 48. The method of claim44 including heating the reactor to a temperature of approximately 200°to 290° C. and controlling the pressure within the reactor such that thepressure does not exceed 350 psi.
 49. The method of claim 48 includingpressurizing the reactor to about 40 to 80 psi with an inert gas takenfrom the group consisting of argon, nitrogen and helium, and wherein thereactor is pressurized to about 40 to 80 psi before the reactor issubstantially heated.
 50. The method of claim 44 including heating theparts of the dead animal to form a gaseous composition and distillingthe gaseous composition to form a fuel.
 51. The method of claim 44wherein the parts of the dead animal include parts from dead fowl. 52.The method of claim 50 including mixing a chemical reactant or achemical waste with the dead animal parts to form an animal-chemicalwaste product that is heated in the reactor.
 53. The method of claim 52including controlling the pH of the animal-chemical waste product toabout 8-12.